SMB Process

ABSTRACT

The present invention provides a chromatographic separation process for recovering a polyunsaturated fatty acid (PUFA) product from a feed mixture, which process comprises the steps of: (i) purifying the feed mixture in a first separation step in a simulated or actual moving bed chromatography apparatus having a plurality of linked chromatography columns containing, as eluent, an aqueous organic solvent, to obtain an intermediate product; and (ii) purifying the intermediate product obtained in (i) in a second separation step using a simulated or actual moving bed chromatography apparatus having a plurality of linked chromatography columns containing, as eluent, an aqueous organic solvent, to obtain the PUFA product; wherein (a) the first and second separation steps are carried out sequentially on the same chromatography apparatus, the intermediate product being recovered between the first and second separation steps and the process conditions in the chromatography apparatus being adjusted between the first and second separation steps such that the PUFA product is separated from different components of the feed mixture in each separation step; or (b) the first and second separation steps are carried out on separate first and second chromatography apparatuses respectively, the intermediate product obtained from the first separation step being introduced into the second chromatography apparatus, and the PUFA product being separated from different components of the feed mixture in each separation step.

The present invention relates to an improved chromatographic separationprocess for purifying polyunsaturated fatty acids (PUFAs) andderivatives thereof. In particular, the present invention relates to animproved simulated or actual moving bed chromatographic separationprocess for purifying PUFAs and derivatives thereof.

Fatty acids, in particular PUFAs, and their derivatives are precursorsfor biologically important molecules, which play an important role inthe regulation of biological functions such as platelet aggregation,inflammation and immunological responses. Thus, PUFAs and theirderivatives may be therapeutically useful in treating a wide range ofpathological conditions including CNS conditions; neuropathies,including diabetic neuropathy; cardiovascular diseases; general immunesystem and inflammatory conditions, including inflammatory skindiseases.

PUFAs are found in natural raw materials, such as vegetable oils andmarine oils. Such PUFAs are, however, frequently present in such oils inadmixture with saturated fatty acids and numerous other impurities.PUFAs should therefore desirably be purified before nutritional orpharmaceutical uses.

Unfortunately, PUFAs are extremely fragile. Thus, when heated in thepresence of oxygen, they are prone to isomerization, peroxidation andoligomerization. The fractionation and purification of PUFA products toprepare pure fatty acids is therefore difficult. Distillation, evenunder vacuum, can lead to non-acceptable product degradation.

Simulated and actual moving bed chromatography are known techniques,familiar to those of skill in the art. The principle of operationinvolves countercurrent movement of a liquid eluent phase and a solidadsorbent phase. This operation allows minimal usage of solvent makingthe process economically viable. Such separation technology has foundseveral applications in diverse areas, including hydrocarbons,industrial chemicals, oils, sugars and APIs.

As is well known, in a conventional stationary bed chromatographicsystem, a mixture whose components are to be separated percolatesthrough a container. The container is generally cylindrical, and istypically referred to as the column. The column contains a packing of aporous material (generally called the stationary phase) exhibiting ahigh permeability to fluids. The percolation velocity of each componentof the mixture depends on the physical properties of that component sothat the components exit from the column successively and selectively.Thus, some of the components tend to fix strongly to the stationaryphase and thus will percolate slowly, whereas others tend to fix weaklyand exit from the column more quickly. Many different stationary bedchromatographic systems have been proposed and are used for bothanalytical and industrial production purposes.

In contrast, a simulated moving bed chromatography apparatus consists ofa number of individual columns containing adsorbent which are connectedtogether in series. Eluent is passed through the columns in a firstdirection. The injection points of the feedstock and the eluent, and theseparated component collection points in the system, are periodicallyshifted by means of a series of valves. The overall effect is tosimulate the operation of a single column containing a moving bed of thesolid adsorbent, the solid adsorbent moving in a countercurrentdirection to the flow of eluent. Thus, a simulated moving bed systemconsists of columns which, as in a conventional stationary bed system,contain stationary beds of solid adsorbent through which eluent ispassed, but in a simulated moving bed system the operation is such as tosimulate a continuous countercurrent moving bed.

Processes and equipment for simulated moving bed chromatography aredescribed in several patents, including U.S. Pat. No. 2,985,589, U.S.Pat. No. 3,696,107, U.S. Pat. No. 3,706,812, U.S. Pat. No. 3,761,533,FR-A-2103302, FR-A-2651148 and FR-A-2651149, the entirety of which areincorporated herein by reference. The topic is also dealt with at lengthin “Preparative and Production Scale Chromatography”, edited by Ganetsosand Barker, Marcel Dekker Inc, New York, 1993, the entirety of which isincorporated herein by reference.

An actual moving bed system is similar in operation to a simulatedmoving bed system. However, rather than shifting the injection points ofthe feed mixture and the eluent, and the separated component collectionpoints by means of a system of valves, instead a series of adsorptionunits (i.e. columns) are physically moved relative to the feed anddrawoff points. Again, operation is such as to simulate a continuouscountercurrent moving bed.

Processes and equipment for actual moving bed chromatography aredescribed in several patents, including U.S. Pat. No. 6,979,402, U.S.Pat. No. 5,069,883 and U.S. Pat. No. 4,764,276, the entirety of whichare incorporated herein by reference.

Purification of PUFA products is particularly challenging. Thus, manysuitable feedstocks for preparing PUFA products are extremely complexmixtures containing a large number of different components with verysimilar retention times in chromatography apparatuses. It is thereforevery difficult to separate certain PUFAs from such feedstocks. However,a high degree of purity of PUFA products is required, particularly forpharmaceutical and nutraceutical applications. Historically, therefore,distillation has been used when high purity PUFA products are required.There are, however, significant drawbacks to using distillation as aseparation technique for delicate PUFAs as discussed above.

As yet, no chromatographic technique has been made available forachieving high purity PUFA products, for example greater than 95 or 97%purity, in particular from commercially available feedstocks such asfish oils.

A typical in a simulated moving bed chromatography apparatus isillustrated with reference to FIG. 1. The concept of a simulated oractual moving bed chromatographic separation process is explained byconsidering a vertical chromatographic column containing stationaryphase S divided into sections, more precisely into four superimposedsub-zones I, II, III and IV going from the bottom to the top of thecolumn. The eluent is introduced at the bottom at IE by means of a pumpP. The mixture of the components A and B which are to be separated isintroduced at IA+B between sub-zone II and sub-zone III. An extractcontaining mainly B is collected at SB between sub-zone I and sub-zoneII, and a raffinate containing mainly A is collected at SA betweensub-zone III and sub-zone IV.

In the case of a simulated moving bed system, a simulated downwardmovement of the stationary phase S is caused by movement of theintroduction and collection points relative to the solid phase. In thecase of an actual moving bed system, simulated downward movement of thestationary phase S is caused by movement of the various chromatographiccolumns relative to the introduction and collection points. In FIG. 1,eluent flows upward and mixture A+B is injected between sub-zone II andsub-zone III. The components will move according to theirchromatographic interactions with the stationary phase, for exampleadsorption on a porous medium. The component B that exhibits strongeraffinity to the stationary phase (the slower running component) will bemore slowly entrained by the eluent and will follow it with delay. Thecomponent A that exhibits the weaker affinity to the stationary phase(the faster running component) will be easily entrained by the eluent.If the right set of parameters, especially the flow rate in eachsub-zone, are correctly estimated and controlled, the component Aexhibiting the weaker affinity to the stationary phase will be collectedbetween sub-zone III and sub-zone IV as a raffinate and the component Bexhibiting the stronger affinity to the stationary phase will becollected between sub-zone I and sub-zone II as an extract.

It will therefore be appreciated that the conventional simulated movingbed system schematically illustrated in FIG. 1 is limited to binaryfractionation.

Accordingly, there is a need for a simulated or actual moving bedchromatographic separation process that can separate PUFAs or theirderivatives from both faster and slower running components (i.e. morepolar and less polar impurities), to produce high purity PUFA productsfrom commercially available feedstocks such as fish oils. It is furtherdesirable that the process should involve inexpensive eluents whichoperate under standard temperature and pressure conditions.

SUMMARY OF THE INVENTION

It has now been surprisingly found that a PUFA product can beeffectively purified from commercially available feedstocks such as fishoils by simulated or actual moving bed apparatus using an aqueousorganic solvent eluent. The present invention therefore provides achromatographic separation process for recovering a polyunsaturatedfatty acid (PUFA) product from a feed mixture, which process comprisesthe steps of:

(i) purifying the feed mixture in a first separation step in a simulatedor actual moving bed chromatography apparatus having a plurality oflinked chromatography columns containing, as eluent, an aqueous organicsolvent, to obtain an intermediate product; and(ii) purifying the intermediate product obtained in (i) in a secondseparation step using a simulated or actual moving bed chromatographyapparatus having a plurality of linked chromatography columnscontaining, as eluent, an aqueous organic solvent, to obtain the PUFAproduct; wherein(a) the first and second separation steps are carried out sequentiallyon the same chromatography apparatus, the intermediate product beingrecovered between the first and second separation steps and the processconditions in the chromatography apparatus being adjusted between thefirst and second separation steps such that the PUFA product isseparated from different components of the feed mixture in eachseparation step; or(b) the first and second separation steps are carried out on separatefirst and second chromatography apparatuses respectively, theintermediate product obtained from the first separation step beingintroduced into the second chromatography apparatus, and the PUFAproduct being separated from different components of the feed mixture ineach separation step.

Also provided is a PUFA product obtainable by the process of the presentinvention.

The PUFA products produced by the process of the present invention areproduced in high yield, and have high purity. Further, the content ofthe distinctive impurities which typically arise from distillation ofPUFAs is very low. As used herein, the term “isomeric impurities” isused to denote those impurities typically produced during thedistillation of PUFA-containing natural oils. These include PUFAisomers, peroxidation and oligomerization products.

DESCRIPTION OF THE FIGURES

FIG. 1 illustrates the basic principles of a simulated or actual movingbed process for separating a binary mixture.

FIG. 2 illustrates a first preferred embodiment of the invention whichis suitable for separating EPA from faster and slower running components(i.e. more polar and less polar impurities).

FIG. 3 illustrates a second preferred embodiment of the invention whichis suitable for separating DHA from faster and slower running components(i.e. more polar and less polar impurities).

FIG. 4 illustrates in more detail the first preferred embodiment of theinvention which is suitable for separating EPA from faster and slowerrunning components (i.e. more polar and less polar impurities).

FIG. 5 illustrates in more detail the second preferred embodiment of theinvention which is suitable for separating DHA from faster and slowerrunning components (i.e. more polar and less polar impurities).

FIG. 6 illustrates in more detail an alternative method for the firstpreferred embodiment of the invention which is suitable for separatingEPA from faster and slower running components (i.e. more polar and lesspolar impurities).

FIG. 7 illustrates in more detail an alternative method for the secondpreferred embodiment of the invention which is suitable for separatingDHA from faster and slower running components (i.e. more polar and lesspolar impurities).

FIG. 8 illustrates a particularly preferred embodiment of the inventionfor purifying EPA from faster and slower running components (i.e. morepolar and less polar impurities).

FIG. 9 illustrates an alternative method for a particularly preferredembodiment of the invention for purifying EPA from faster and slowerrunning components (i.e. more polar and less polar impurities).

FIG. 10 illustrates three ways in which the chromatographic separationprocess of the invention may be carried out.

FIG. 11 shows a GC analysis of an EPA-rich feedstock which can suitablybe used as the feed mixture in the process of the present invention.

FIG. 12 shows a GC analysis of the raffinate intermediate productobtained in the first separation step of a process according to thepresent invention.

FIG. 13 shows a GC analysis of the final EPA product from the secondseparation step of a process according to the present invention.

FIG. 14 shows a GC analysis of the final EPA product from the secondseparation step of a process according to the present invention.

FIG. 15 shows a GC FAMES trace of a DHA product produced by SMB.

FIG. 16 shows a GC FAMES trace of a DHA product produced bydistillation.

DETAILED DESCRIPTION OF THE INVENTION

The chromatographic separation process of the invention is typicallyother than a chromatographic separation process for recovering apolyunsaturated fatty acid (PUFA) product, from a feed mixture, whichprocess comprises introducing the feed mixture to a simulated or actualmoving bed chromatography apparatus having a plurality of linkedchromatography columns containing, as eluent, an aqueous alcohol,wherein the apparatus has a plurality of zones comprising at least afirst zone and second zone, each zone having an extract stream and araffinate stream from which liquid can be collected from said pluralityof linked chromatography columns, and wherein (a) a raffinate streamcontaining the PUFA product together with more polar components iscollected from a column in the first zone and introduced to anonadjacent column in the second zone, and/or (b) an extract streamcontaining the PUFA product together with less polar components iscollected from a column in the second zone and introduced to anonadjacent column in the first zone, said PUFA product being separatedfrom different components of the feed mixture in each zone.

As used herein in this embodiment, the term “zone” refers to a pluralityof linked chromatography columns containing, as eluent, an aqueousalcohol, and having one or more injection points for a feed mixturestream, one or more injection points for water and/or alcohol, araffinate take-off stream from which liquid can be collected from saidplurality of linked chromatography columns, and an extract take-offstream from which liquid can be collected from said plurality of linkedchromatography columns Typically, each zone has only one injection pointfor a feed mixture. In one embodiment, each zone has only one injectionpoint for the aqueous alcohol eluent. In another embodiment, each zonehas two or more injection points for water and/or alcohol.

Further details of this embodiment are to be found in internationalpatent application no. PCT/GB10/002339, the entirety of which isincorporated herein by reference. The chromatographic separation processof the invention is typically other than the processes disclosed inPCT/GB10/002339.

As used herein, the term “PUFA product” refers to a product comprisingone or more polyunsaturated fatty acids (PUFAs), and/or derivativesthereof, typically of nutritional or pharmaceutical significance.Typically, the PUFA product is a single PUFA or derivative thereof.Alternatively, the PUFA product is a mixture of two or more PUFAs orderivatives thereof, for example two.

The term “polyunsaturated fatty acid” (PUFA) refers to fatty acids thatcontain more than one double bond. Such PUFAs are well known to theperson skilled in the art. As used herein, a PUFA derivative is a PUFAin the form of a mono-, di- or tri-glyceride, ester, phospholipid,amide, lactone, or salt. Triglycerides and esters are preferred. Estersare more preferred. Esters are typically alkyl esters, preferably C₁-C₆alkyl esters, more preferably C₁-C₄ alkyl esters. Examples of estersinclude methyl and ethyl esters. Ethyl esters are most preferred.

Typically, the PUFA product comprises at least one ω-3 or ω-6 PUFA,preferably at least one ω-3 PUFA. Examples of ω-3 PUFAs includealpha-linolenic acid (ALA), stearidonic acid (SDA), eicosatrienoic acid(ETE), eicosatetraenoic acid (ETA), eicosapentaenoic acid (EPA),docosapentaenoic acid (DPA) and docosahexaenoic acid (DHA). SDA, EPA,DPA and DHA are preferred. EPA and DHA are more preferred. Examples ofω-6 PUFAs include linoleic acid (LA), gamma-linolenic acid (GLA),eicosadienoic acid, dihomo-gamma-linolenic acid (DGLA), arachidonic acid(ARA), docosadienoic acid, adrenic acid and docosapentaenoic (ω-6) acid.LA, ARA, GLA and DGLA are preferred.

In one embodiment, the PUFA product is EPA and/or EPA ethyl ester (EE)

In another embodiment, the PUFA product is DHA and/or DHA ethyl ester(EE).

In a yet further embodiment, the PUFA product is a mixture of EPA andDHA and/or EPA EE and DHA EE.

In a most preferred embodiment, the PUFA product is EPA or EPA ethylester which is produced in greater than 90% purity, preferably greaterthan 95% purity, and more preferably greater than 97% purity.

Typically, in addition to said PUFA product, an additional secondaryPUFA product is collected in the chromatographic separation process ofthe invention. Preferably, the PUFA product is EPA and the additionalsecondary PUFA product is DHA.

In a further embodiment of the invention, the apparatus is configured tocollect a PUFA product which is a concentrated mixture of EPA and DHA.Thus, a feed mixture is used which contains EPA, DHA, components whichare more polar than EPA and DHA, and components which are less polarthan EPA and DHA. In the first separation step, less polar material thanEPA and DHA is typically removed. In the second separation step,material which is more polar than EPA and DHA is typically removed, anda concentrated mixture of EPA and DHA is collected as the PUFA product.

Suitable feed mixtures for fractionating by the process of the presentinvention may be obtained from natural sources including vegetable andanimal oils and fats, and from synthetic sources including oils obtainedfrom genetically modified plants, animals and micro organisms includingyeasts. Examples include fish oils, algal and microalgal oils and plantoils, for example borage oil, Echium oil and evening primrose oil. Inone embodiment, the feed mixture is a fish oil. In another embodiment,the feed mixture is an algal oil. Algal oils are particularly suitablewhen the desired PUFA product is EPA and/or DHA. Genetically modifiedSafflower oil is particularly suitable when the desired PUFA product isGLA. Genetically modified yeast is particularly suitable when thedesired PUFA product is EPA.

In a particularly preferred embodiment the feed mixture is a fish oil orfish-oil derived feedstock. It has advantageously been found that when afish-oil or fish-oil derived feed stock is used, an EPA or EPA ethylester PUFA product can be produced by the process of the presentinvention in greater than 90% purity, preferably greater than 95%purity, and more preferably greater than 97% purity.

The feed mixture may undergo chemical treatment before fractionation bythe process of the invention. For example, it may undergo glyceridetransesterification or glyceride hydrolysis followed in certain cases byselective processes such as crystallisation, molecular distillation,urea fractionation, extraction with silver nitrate or other metal saltsolutions, iodolactonisation or supercritical fluid fractionation.Alternatively, a feed mixture may be used directly with no initialtreatment step.

The feed mixtures typically contain the PUFA product and at least onemore polar component and at least one less polar component. The lesspolar components have a stronger adherence to the adsorbent used in theprocess of the present invention than does the PUFA product. Duringoperation, such less polar components typically move with the solidadsorbent phase in preference to the liquid eluent phase. The more polarcomponents have a weaker adherence to the adsorbent used in the processof the present invention than does the PUFA product. During operation,such more polar components typically move with the liquid eluent phasein preference to the solid adsorbent phase. In general, more polarcomponents will be separated into a raffinate stream, and less polarcomponents will be separated into an extract stream.

Examples of the more and less polar components include (1) othercompounds occurring in natural oils (e.g. marine oils or vegetableoils), (2) byproducts formed during storage, refining and previousconcentration steps and (3) contaminants from solvents or reagents whichare utilized during previous concentration or purification steps.

Examples of (1) include other unwanted PUFAs; saturated fatty acids;sterols, for example cholesterol; vitamins; and environmentalpollutants, such as polychlorobiphenyl (PCB), polyaromatic hydrocarbon(PAH) pesticides, chlorinated pesticides, dioxines and heavy metals.PCB, PAH, dioxines and chlorinated pesticides are all highly non-polarcomponents.

Examples of (2) include isomers and oxidation or decomposition productsfrom the PUFA product, for instance, auto-oxidation polymeric productsof fatty acids or their derivatives.

Examples of (3) include urea which may be added to remove saturated ormono-unsaturated fatty acids from the feed mixture.

Preferably, the feed mixture is a PUFA-containing marine oil (e.g. afish oil), more preferably a marine oil (e.g. a fish oil) comprising EPAand/or DHA.

A typical feed mixture for preparing concentrated EPA (EE) by theprocess of the present invention comprises 50-75% EPA (EE), 0 to 10% DHA(EE), and other components including other essential ω-3 and ω-6 fattyacids.

A preferred feed mixture for preparing concentrated EPA (EE) by theprocess of the present invention comprises 55% EPA (EE), 5% DHA (EE),and other components including other essential ω-3 and ω-6 fatty acids.DHA (EE) is less polar than EPA(EE).

A typical feed mixture for preparing concentrated DHA (EE) by theprocess of the present invention comprises 50-75% DHA (EE), 0 to 10% EPA(EE), and other components including other essential ω-3 and ω-6 fattyacids.

A preferred feed mixture for preparing concentrated DHA (EE) by theprocess of the present invention comprises 75% DHA (EE), 7% EPA (EE) andother components including other essential ω-3 and ω-6 fatty acids. EPA(EE) is more polar than DHA (EE).

A typical feed mixture for preparing a concentrated mixture of EPA (EE)and DHA (EE) by the process of the present invention comprises greaterthan 33% EPA (EE), and greater than 22% DHA (EE).

Each separation step of the process of the present invention is carriedout in a simulated or actual moving bed chromatography apparatus.

Any known simulated or actual moving bed chromatography apparatus may beutilised for the purposes of the method of the present invention, aslong as the apparatus is used in accordance with the process of thepresent invention. Those apparatuses described in U.S. Pat. No.2,985,589, U.S. Pat. No. 3,696,107, U.S. Pat. No. 3,706,812, U.S. Pat.No. 3,761,533, FR-A-2103302, FR-A-2651148, FR-A-2651149, U.S. Pat. No.6,979,402, U.S. Pat. No. 5,069,883 and U.S. Pat. No. 4,764,276 may allbe used if configured in accordance with the process of the presentinvention.

As used herein, the term “simulated or actual moving bed chromatographyapparatus” typically refers to a plurality of linked chromatographycolumns containing, as eluent, an aqueous organic solvent, and havingone or more injection points for a feed mixture stream, one or moreinjection points for water and/or organic solvent, a raffinate take-offstream from which liquid can be collected from said plurality of linkedchromatography columns, and an extract take-off stream from which liquidcan be collected from said plurality of linked chromatography columns.

The chromatography apparatus used in each step of the process of thepresent invention has a single array of chromatography columns linked inseries containing, as eluent, an aqueous organic solvent. Typically,each of the chromatography columns are linked to the two columns in theapparatus adjacent to that column. Thus, the output from a given columnin the array is connected to the input of the adjacent column in thearray, which is downstream with respect to the flow of eluent in thearray. Thus, eluent can flow around the array of linked chromatographycolumns. Typically, none of the chromatography columns are linked tonon-adjacent columns in the apparatus.

As used herein the term “nonadjacent” refers to columns, in for examplethe same apparatus, separated by one or more columns, preferably 3 ormore columns, more preferably 5 or more columns, most preferably about 5columns.

Typically, each apparatus has only one injection point for a feedmixture. In one embodiment, each apparatus has only one injection pointfor the aqueous organic solvent eluent. In another embodiment, eachapparatus has two or more injection points for water and/or organicsolvent.

The term “raffinate” is well known to the person skilled in the art. Inthe context of actual and simulated moving bed chromatography it refersto the stream of components that move more rapidly with the liquideluent phase compared with the solid adsorbent phase. Thus, a raffinatestream is typically enriched with more polar components, and depleted ofless polar components compared with a feed stream.

The term “extract” is well known to the person skilled in the art. Inthe context of actual and simulated moving bed chromatography it refersto the stream of components that move more rapidly with the solidadsorbent phase compared with the liquid eluent phase. Thus, an extractstream is typically enriched with less polar components, and depleted ofmore polar components compared with a feed stream.

The number of columns used in each apparatus is not particularlylimited. A skilled person would easily be able to determine anappropriate number of columns to use. The number of columns is typically4 or more, preferably 6 or more, more preferably 8 or more, for example4, 5, 6, 7, 8, 9, or 10 columns. In preferred embodiment, 5 or 6columns, more preferably 6 columns. are used. In another preferredembodiment, 7 or 8 columns, more preferably 8 columns are used.Typically, there are no more than 25 columns, preferably no more than20, more preferably no more than 15.

The chromatographic apparatuses used in the first and second separationsteps typically contain the same number of columns. For certainapplications they may have different numbers of columns.

The dimensions of the columns used in the apparatus are not particularlylimited, and will depend on the volume of feed mixture to be purified. Askilled person would easily be able to determine appropriately sizedcolumns to use. The diameter of each column is typically between 10 and1000 mm, preferably between 10 and 500 mm, more preferably between 25and 250 mm, even more preferably between 50 and 100 mm, and mostpreferably between 70 and 80 mm. The length of each column is typicallybetween 10 and 300 cm, preferably between 10 and 200 cm, more preferablybetween 25 and 150 cm, even more preferably between 70 and 110 cm, andmost preferably between 80 and 100 cm.

The columns in the chromatographic apparatuses used in the first andsecond separation steps typically have identical dimensions but may, forcertain applications, have different dimensions.

The flow rates to the column are limited by maximum pressures across theseries of columns and will depend on the column dimensions and particlesize of the solid phases. One skilled in the art will easily be able toestablish the required flow rate for each column dimension to ensureefficient desorption. Larger diameter columns will in general needhigher flows to maintain linear flow through the columns.

For the typical column sizes outlined above, typically the flow rate ofeluent into the chromatographic apparatus used in the first separationstep is from 1 to 4.5 L/min, preferably from 1.5 to 2.5 L/min.Typically, the flow rate of the extract from the chromatographicapparatus used in the first separation step is from 0.1 to 2.5 L/min,preferably from 0.5 to 2.25 L/min. In embodiments where part of theextract from the first separation step is recycled back into theapparatus used in the first separation step, the flow rate of recycle istypically from 0.7 to 1.4 L/min, preferably about 1 L/min. Typically,the flow rate of the raffinate from the chromatographic apparatus usedin the first separation step is from 0.2 to 2.5 L/min, preferably from0.3 to 2.0 L/min. In embodiments where part of the raffinate from thefirst separation step is recycled back into the apparatus used in thefirst separation step, the flow rate of recycle is typically from 0.3 to1.0 L/min, preferably about 0.5 L/min. Typically, the flow rate ofintroduction of the feed mixture into the chromatographic apparatus usedin the first separation step is from 5 to 150 mL/min, preferably from 10to 100 mL/min, more preferably from 20 to 60 mL/min.

For the typical column sizes outlined above, typically the flow rate ofeluent into the chromatographic apparatus used in the second separationstep is from 1 to 4 L/min, preferably from 1.5 to 3.5 L/min. Typically,the flow rate of the extract from the chromatographic apparatus used inthe second separation step is from from 0.5 to 2 L/min, preferably from0.7 to 1.9 L/min. In embodiments where part of the extract from thesecond separation step is recycled back into the apparatus used in thesecond separation step, the flow rate of recycle is typically from 0.6to 1.4 L/min, preferably from 0.7 to 1.1 L/min, more preferably about0.9 L/min. Typically, the flow rate of the raffinate from thechromatographic apparatus used in the second separation step is from 0.5to 2.5 L/min, preferably from 0.7 to 1.8 L/min, more preferably about1.4 L/min. In embodiments where part of the raffinate from the secondseparation step is recycled back into the apparatus used in the secondseparation step, the flow rate of recycle is typically from 0.3 to 1.0L/min, preferably about 0.5 L/min.

As the skilled person will appreciate, references to rates at whichliquid is collected or removed via the various extract and raffinatestreams refer to volumes of liquid removed in an amount of time,typically L/minute. Similarly, references to rates at which liquid isrecycled back into an apparatus, typically to an adjacent column in theapparatus, refer to volumes of liquid recycled in an amount of time,typically L/minute.

The step time, i.e. the time between shifting the points of injection ofthe feed mixture and eluent, and the various take off points of thecollected fractions, is not particularly limited, and will depend on thenumber and dimensions of the columns used, and the flow rate through theapparatus. A skilled person would easily be able to determineappropriate step times to use in the process of the present invention.The step time is typically from 100 to 1000 seconds, preferably from 200to 800 seconds, more preferably from about 250 to about 750 seconds. Insome embodiments, a step time of from 100 to 400 seconds, preferably 200to 300 seconds, more preferably about 250 seconds, is appropriate. Inother embodiments, a step time of from 600 to 900 seconds, preferably700 to 800 seconds, more preferably about 750 seconds is appropriate.

In the process of the present invention, actual moving bedchromatography is preferred.

Conventional adsorbents known in the art for actual and simulated movingbed systems may be used in the process of the present invention. Eachchromatographic column may contain the same or a different adsorbent.Typically, each column contains the same adsorbent. Examples of suchcommonly used materials are polymeric beads, preferably polystyrenereticulated with DVB (divinylbenzene); and silica gel, preferablyreverse phase bonded silica gel with C8 or C18 alkanes, especially C18.C18 bonded reverse phase silica gel is preferred. The adsorbent used inthe process of the present invention is preferably non-polar.

The shape of the adsorbent stationary phase material may be, forexample, spherical or nonspherical beads, preferably substantiallyspherical beads. Such beads typically have a diameter of 5 to 500microns, preferably 10 to 500 microns, more preferably 15 to 500microns, more preferably 40 to 500 microns, more preferably 100 to 500microns, more preferably 250 to 500 microns, even more preferably 250 to400 microns, most preferably 250 to 350 microns. In some embodiments,beads with a diameter of 5 to 35 microns may be used, typically 10 to 30microns, preferably 15 to 25 microns. Some preferred particle sizes aresomewhat larger than particle sizes of beads used in the past insimulated and actual moving bed processes. Use of larger particlesenables a lower pressure of eluent to be used in the system. This, inturn, has advantages in terms of cost savings, efficiency and lifetimeof the apparatus. It has surprisingly been found that adsorbent beads oflarge particle size may be used in the process of the present invention(with their associated advantages) without any loss in resolution.

The adsorbent typically has a pore size of from 10 to 50 nm, preferably15 to 45 nm, more preferably 20 to 40 nm, most preferably 25 to 35 nm.

Typically, the process of the present invention is conducted at from 15to 55° C., preferably at from 20 to 40° C., more preferably at about 30°C. Thus, the process is typically carried out at room temperature, butmay be conducted at elevated temperatures.

The process of the present invention comprises a first and secondseparation step.

These two steps can easily be carried out on a single chromatographicapparatus. Thus, in one embodiment, (a) the first and second separationsteps are carried out sequentially on the same chromatography apparatus,the intermediate product being recovered between the first and secondseparation steps and the process conditions in the chromatographyapparatus being adjusted between the first and second separation stepssuch that the PUFA product is separated from different components of thefeed mixture in each separation step. A preferred embodiment of thisseparation process is shown as FIG. 10 a. Thus, the first separationstep (left hand side) is carried out on an SMB apparatus having 8columns. Between the first and second separation steps the intermediateproduct is recovered in, for example, a container, the processconditions in the chromatography apparatus are adjusted such that thePUFA product is separated from different components of the feed mixturein each separation step. The second separation step (right hand side) isthen carried out on the same SMB apparatus having 8 columns.

In embodiment (a), adjusting the process conditions typically refers toadjusting the process conditions in the apparatus as a whole, i.e.physically modifying the apparatus so that the conditions are different.It does not refer to simply reintroducing the intermediate product backinto a different part of the same apparatus where the process conditionsmight happen to be different.

Alternatively, first and second separate chromatographic apparatuses canbe used in the first and second separation steps. Thus, in anotherembodiment, (b) the first and second separation steps are carried out onseparate first and second chromatography apparatuses respectively, theintermediate product obtained from the first separation step beingintroduced into the second chromatography apparatus, and the PUFAproduct being separated from different components of the feed mixture ineach separation step.

In embodiment (b), the two separation steps may either be carried outsequentially or simultaneously.

Thus, in embodiment (b) in the case where the two separation steps arecarried out sequentially, the first and second separation steps arecarried out sequentially on separate first and second chromatographyapparatuses respectively, the intermediate product being recoveredbetween the first and second separation steps and the process conditionsin the first and second chromatography apparatuses being adjusted suchthat the PUFA product is separated from different components of the feedmixture in each separation step. A preferred embodiment of thisseparation process is shown as FIG. 10 b. Thus, the first separationstep (left hand side) is carried out on an SMB apparatus having 8columns, one to eight. Between the first and second separation steps theintermediate product is recovered, for example in a container, and thenintroduced into a second separate SMB apparatus. The second separationstep (right hand side) is carried out on the second separate SMBapparatus which has 8 columns, nine to sixteen. The process conditionsin the two chromatography apparatuses are adjusted such that the PUFAproduct is separated from different components of the feed mixture ineach separation step.

In embodiment (b) in the case where the two separation steps are carriedour simultaneously, the first and second separation steps are carriedout on separate first and second chromatography apparatusesrespectively, the intermediate product being introduced into thechromatography apparatus used in the second separation step, and theprocess conditions in the first and second chromatography apparatusesbeing adjusted such that the PUFA product is separated from differentcomponents of the feed mixture in each separation step. A preferredembodiment of this separation process is shown as FIG. 10 c. Thus, thefirst separation step (left hand side) is carried out on an SMBapparatus having 8 columns, one to eight. The intermediate productobtained in the first separation step is then introduced into the secondseparate chromatography apparatus used in the second separation step.The intermediate product may be passed from the first separation step tothe second separation step directly or indirectly, for example via acontainer. The second separation step (right hand side) is carried outon the second separate SMB apparatus which has 8 columns, nine tosixteen. The process conditions in the two chromatography apparatusesare adjusted such that the PUFA product is separated from differentcomponents of the feed mixture in each separation step.

In embodiment (b) in the case where the two separation steps are carriedour simultaneously, eluent circulates separately in the two separatechromatographic apparatuses. Thus, eluent is not shared between the twoseparate chromatographic apparatuses other than what eluent may bepresent as solvent in the intermediate product which is purified in thesecond separation step, and which is introduced into the chromatographicapparatus used in the second separation step. Chromatographic columnsare not shared between the two separate chromatographic apparatuses usedin the first and second separation steps.

After the intermediate product is obtained in the first separation step,the aqueous organic solvent eluent may be partly or totally removedbefore the intermediate product is purified in the second separationstep. Alternatively, the intermediate product may be purified in thesecond separation step without the removal of any solvent present.

As mentioned above, the PUFA product is separated from differentcomponents of the feed mixture in each separation step. In embodiment(a), the process conditions of the single SMB apparatus used in bothseparation steps are adjusted between the first and second separationsteps such that the PUFA product is separated from different componentsof the feed mixture in each separation step. In embodiment (b), theprocess conditions in the two separate chromatography apparatuses usedin the first and second separation steps are set such that the PUFAproduct is separated from different components of the feed mixture ineach separation step.

Thus, the process conditions in the first and second separation stepsvary. The process conditions which vary may include, for example, thesize of the columns used, the number of columns used, the packing usedin the columns, the step time of the SMB apparatus, the temperature ofthe apparatus, or the flow rates used in the apparatus, in particularthe recycle rate of liquid collected via the extract or raffinatestreams.

The intermediate product obtained in the first separation step istypically enriched in the PUFA product compared to the feed mixture.

The intermediate product obtained in the first separation step is thenintroduced into the chromatographic apparatus used in the secondseparation step.

The intermediate product is typically collected as the raffinate orextract stream from the chromatographic apparatus used in the firstseparation process.

Typically, the intermediate product is collected as the raffinate streamin the first separation step, and the PUFA product is collected as theextract stream in the second separation step. Thus, the raffinate streamcollected in the first separation step is used as the feed mixture inthe second separation step. The raffinate stream collected in the firstseparation step typically contains the PUFA product together with morepolar components.

Alternatively, the intermediate product is collected as the extractstream in the first separation step, and the PUFA product is collectedas the raffinate stream in the second separation step. Thus, the extractstream collected in the first separation step is used as the feedmixture in the second separation step. The extract stream collected inthe first separation step typically contains the PUFA product togetherwith less polar components.

The PUFA product is separated from different components of the feedmixture in each separation step. Typically, the components separated ineach separation step of the process of the present invention havedifferent polarities.

Preferably, the PUFA product is separated from less polar components ofthe feed mixture in the first separation step, and the PUFA product isseparated from more polar components of the feed mixture in the secondseparation step.

Typically, (a) part of the extract stream from the apparatus used in thefirst separation step is recycled back into the apparatus used in thefirst separation step; and/or (b) part of the raffinate stream from theapparatus used in the first separation step is recycled back into theapparatus used in the first separation step; and/or (c) part of theextract stream from the apparatus used in the second separation step isrecycled back into the apparatus used in the second separation step;and/or (d) part of the raffinate stream from the apparatus used in thesecond separation step is recycled back into the apparatus used in thesecond separation step.

Preferably, (a) part of the extract stream from the apparatus used inthe first separation step is recycled back into the apparatus used inthe first separation step; and (b) part of the raffinate stream from theapparatus used in the first separation step is recycled back into theapparatus used in the first separation step; and (c) part of the extractstream from the apparatus used in the second separation step is recycledback into the apparatus used in the second separation step; and (d) partof the raffinate stream from the apparatus used in the second separationstep is recycled back into the apparatus used in the second separationstep.

This recycle involves feeding part of the extract or raffinate streamout of the chromatography apparatus used in the first or secondseparation step back into the apparatus used in that step, typicallyinto an adjacent column. This adjacent column is the adjacent columnwhich is downstream with respect to the flow of eluent in the system.

The rate at which liquid collected via the extract or raffinate streamin the first or second separation steps is recycled back into thechromatography apparatus used in that step is the rate at which liquidcollected via that stream is fed back into the apparatus used in thatstep, typically into an adjacent column, i.e. the downstream column withrespect to the flow of eluent in the system.

This can be seen with reference to a preferred embodiment in FIG. 9. Therate of recycle of extract in the first separation step is the rate atwhich extract collected from the bottom of column 2 of thechromatographic apparatus used in the first separation step is fed intothe top of column 3 of the chromatographic apparatus used in the firstseparation step, i.e. the flow rate of liquid into the top of column 3of the chromatographic apparatus used in the first separation step.

The rate of recycle of extract in the second separation step is the rateat which extract collected at the bottom of column 2 of thechromatographic apparatus used in the second separation step is fed intothe top of column 3 of the chromatographic apparatus used in the secondseparation step, i.e. the flow rate of liquid into the top of column 3of the chromatographic apparatus used in the second separation step.

Recycle of the extract and/or raffinate streams in the first and/orsecond separation steps is typically effected by feeding the liquidcollected via that stream in that separation step into a container, andthen pumping an amount of that liquid from the container back into theapparatus used in that separation step, typically into an adjacentcolumn. In this case, the rate of recycle of liquid collected via aparticular extract or raffinate stream in the first and/or secondseparation steps, typically back into an adjacent column, is the rate atwhich liquid is pumped out of the container back into the chromatographyapparatus, typically into an adjacent column.

As the skilled person will appreciate, the amount of liquid beingintroduced into a chromatography apparatus via the eluent and feedstockstreams is balanced with the amount of liquid removed from theapparatus, and recycled back into the apparatus.

Thus, with reference to FIG. 9, for the extract stream, the flow rate ofeluent (desorbent) into the chromatographic apparatus(es) used in thefirst and second separation steps (D) is equal to the rate at whichliquid collected via the extract stream in that separation stepaccumulates in a container (E1 and E2) added to the rate at whichextract is recycled back into the chromatographic apparatus used in thatparticular separation step (D-E1 and D-E2).

For the raffinate stream from a separation step, the rate at whichextract is recycled back into the chromatographic apparatus used in thatparticular separation step (D-E1 and D-E2) added to the rate at whichfeedstock is introduced into the chromatographic apparatus used in thatparticular separation step (F and R1) is equal to the rate at whichliquid collected via the raffinate stream in that particular separationstep accumulates in a container (R1 and R2) added to the rate at whichraffinate is recycled back into the chromatographic apparatus used inthat particular separation step (D+F-E1-R1 and D+R1-E2-R2).

The rate at which liquid collected from a particular extract orraffinate stream from a chromatography apparatus accumulates in acontainer can also be thought of as the net rate of removal of thatextract or raffinate stream from that chromatography apparatus.

Typically, the rate at which liquid collected via the extract andraffinate streams in the first separation step is recycled back into theapparatus used in that separation step is adjusted such that the PUFAproduct can be separated from different components of the feed mixturein each separation step.

Typically, the rate at which liquid collected via the extract andraffinate streams in the second separation step is recycled back intothe apparatus used in that separation step is adjusted such that thePUFA product can be separated from different components of the feedmixture in each separation step.

Preferably, the rate at which liquid collected via the extract andraffinate streams in each separation step is recycled back into theapparatus used in that separation step is adjusted such that the PUFAproduct can be separated from different components of the feed mixturein each separation step.

Typically, the rate at which liquid collected via the extract stream inthe first separation step is recycled back into the chromatographyapparatus used in the first separation step differs from the rate atwhich liquid collected via the extract stream in the second separationstep is recycled back into the chromatography apparatus used in thesecond separation step, and/or the rate at which liquid collected viathe raffinate stream in the first separation step is recycled back intothe chromatography apparatus used in the first separation step differsfrom the rate at which liquid collected via the raffinate stream in thesecond separation step is recycled back into the chromatographyapparatus used in the second separation step.

Varying the rate at which liquid collected via the extract and/orraffinate streams in the first or second separation steps is recycledback into the apparatus used in that particular separation step has theeffect of varying the amount of more polar and less polar componentspresent in the extract and raffinate streams. Thus, for example, a lowerextract recycle rate results in fewer of the less polar components inthat separation step being carried through to the raffinate stream. Ahigher extract recycle rate results in more of the less polar componentsin that separation step being carried through to the raffinate stream.

This can be seen, for example, in the specific embodiment of theinvention shown in FIG. 6. The rate at which liquid collected via theextract stream in the first separation step is recycled back into thechromatographic apparatus used in that separation step (D-E1) willaffect to what extent any of component A is carried through to theraffinate stream in the first separation step (R1).

Typically, the rate at which liquid collected via the extract stream inthe first separation step is recycled back into the chromatographicapparatus used in the first separation step is faster than the rate atwhich liquid collected via the extract stream in the second separationstep is recycled back into the chromatographic apparatus used in thesecond separation step. Preferably, a raffinate stream containing thePUFA product together with more polar components is collected from thefirst separation step and purified in a second separation step, and therate at which liquid collected via the extract stream in the firstseparation step is recycled back into the chromatographic apparatus usedin the first separation step is faster than the rate at which liquidcollected via the extract stream in the second separation step isrecycled back into the chromatographic apparatus used in the secondseparation step.

Alternatively, the rate at which liquid collected via the extract streamin the first separation step is recycled back into the chromatographicapparatus used in the first separation step is slower than the rate atwhich liquid collected via the extract stream in the second separationstep is recycled back into the chromatographic apparatus used in thesecond separation step.

Typically, the rate at which liquid collected via the raffinate streamin the first separation step is recycled back into the chromatographicapparatus used in the first separation step is faster than the rate atwhich liquid collected via the raffinate stream in the second separationstep is recycled back into the chromatographic apparatus used in thesecond separation step. Preferably, an extract stream containing thePUFA product together with less polar components is collected from thefirst separation step and purified in a second separation step, and therate at which liquid collected via the raffinate stream in the firstseparation step is recycled back into the chromatographic apparatus usedin the first separation step is faster than the rate at which liquidcollected via the raffinate stream in the second separation step isrecycled back into the chromatographic apparatus used in the secondseparation step.

Alternatively, the rate at which liquid collected via the raffinatestream in the first separation step is recycled back into thechromatographic apparatus used in the first separation step is slowerthan the rate at which liquid collected via the raffinate stream in thesecond separation step is recycled back into the chromatographicapparatus used in the second separation step.

In embodiments where recycle rates are adjusted such that the PUFAproduct can be separated from different components of the feed mixturein each separation step, the water:organic solvent ratio of the eluentsused in each separation step may be the same or different. Typically,the water:organic solvent ratio of the eluent in each separation step isfrom 0.5:99.5 to 5.5:94.5 parts by volume.

The eluent used in the process of the present invention is an aqueousorganic solvent.

The aqueous organic solvent typically comprises water and one or morealcohols, ethers, esters, ketones or nitriles, or mixtures thereof.

Alcohol solvents are well known to the person skilled in the art.Alcohols are typically short chain alcohols. Alcohols typically are offormula ROH, wherein R is a straight or branched C₁-C₆ alkyl group. TheC₁-C₆ alkyl group is preferably unsubstituted. Examples of alcoholsinclude methanol, ethanol, n-propanol, i-propanol, n-butanol, i-butanol,s-butanol and t-butanol. Methanol and ethanol are preferred. Methanol ismore preferred.

Ether solvents are well known to the person skilled in the art. Ethersare typically short chain ethers. Ethers typically are of formulaR—O—R′, wherein R and R′ are the same or different and represent astraight or branched C₁-C₆ alkyl group. The C₁-C₆ alkyl group ispreferably unsubstituted. Preferred ethers include diethylether,diisopropylether, and methyl t-butyl ether (MTBE).

Ester solvents are well known to the person skilled in the art. Estersare typically short chain esters. Esters typically are of formulaR—(C═O)O—R′, wherein R and R′ are the same or different and represent astraight or branched C₁-C₆ alkyl group. Preferred esters includemethylacetate and ethylacetate.

Ketone solvents are well known to the person skilled in the art. Ketonesare typically short chain ketones. Ketones typically are of formulaR—(C═O)—R′, wherein R and R′ are the same or different and represent astraight or branched C₁-C₆ alkyl group. The C₁-C₆ alkyl group ispreferably unsubstituted. Preferred ketones include acetone,methylethylketone and methyl isobutyl ketone (MIBK).

Nitrile solvents are well known to the person skilled in the art.Nitriles are typically short chain nitriles. Nitriles typically are offormula R—CN, wherein R represents a straight or branched C₁-C₆ alkylgroup. The C₁-C₆ alkyl group is preferably unsubstituted. Preferrednitriles include acetonitrile.

Typically, the aqueous organic solvent is aqueous alcohol or aqueousacetonitrile.

The aqueous organic solvent is preferably aqueous methanol or aqueousacetonitrile. Aqueous methanol is more preferred.

Typically, the eluent is not in a supercritical state. Typically, theeluent is a liquid.

Typically, the average water:organic solvent ratio, for examplewater:methanol ratio, of the eluent in the entire apparatus is from0.1:99.9 to 9:91 parts by volume, preferably from 0.25:99.75 to 7:93parts by volume, more preferably from 0.5:99.5 to 6:94 parts by volume.

When the aqueous organic solvent is aqueous acetonitrile, the eluenttypically contains up to 30 wt % water, remainder acetonitrile.Preferably, the eluent contains from 5 to 25 wt % water, remainderacetonitrile. More preferably, the eluent contains from 10 to 20 wt %water, remainder acetonitrile. Even more preferably, the eluent containsfrom 15 to 25 wt % water, remainder acetonitrile.

In a particularly preferred embodiment, either (1) the intermediateproduct containing the PUFA product together with more polar componentsis collected as the raffinate stream in the first separation step, andthe PUFA product is collected as the extract stream in the secondseparation step; or

(2) the intermediate product containing the PUFA product together withless polar components is collected as the extract stream in the firstseparation step, and the PUFA product is collected as the raffinatestream in the second separation step.

Particularly preferred embodiment (1) is suitable for purifying EPA froma feed mixture.

This particularly preferred embodiment (1) is illustrated in FIG. 2. Afeed mixture F comprising the PUFA product (B) and more polar (C) andless polar (A) components is purified in the first separation step. Inthe first separation step, the less polar components (A) are removed asextract stream E1. The PUFA product (B) and more polar components (C)are collected as raffinate stream R1. Raffinate stream R1 is theintermediate product which is then purified in the second separationstep. In the second separation step, the more polar components (C) areremoved as raffinate stream R2. The PUFA product (B) is collected asextract stream E2.

This embodiment is illustrated in more detail in FIG. 4. FIG. 4 isidentical to FIG. 2, except that the points of introduction of theorganic solvent desorbent (D) and water (W) into each chromatographicapparatus are shown. The organic solvent desorbent (D) and water (W)together make up the eluent. The (D) phase is typically essentially pureorganic solvent, but may, in certain embodiments be an organicsolvent/water mixture comprising mainly organic solvent. The (W) phaseis typically essentially pure water, but may, in certain embodiments bean organic solvent/water mixture comprising mainly water, for example a98% water/2% methanol mixture.

A further illustration of this particularly preferred embodiment isshown in FIG. 6. Here there is no separate water injection point, andinstead an aqueous organic solvent desorbent is injected at (D).

The separation into raffinate and extract stream can be aided by varyingthe desorbing power of the eluent within each chromatographic apparatus.This can be achieved by introducing the organic solvent (or organicsolvent rich) component of the eluent and the water (or water rich)component at different points in each chromatographic apparatus. Thus,typically, the organic solvent is introduced upstream of the extracttake-off point and the water is introduced between the extract take-offpoint and the point of introduction of the feed into the chromatographicapparatus, relative to the flow of eluent in the system. This is shownin FIG. 4.

Typical solvents for use in this most preferred embodiment are aqueousalcohols or aqueous acetonitrile, preferably aqueous methanol.

The separation can be aided by varying the rates at which liquidcollected via the extract and raffinate streams in the first and secondseparation steps is recycled back into the chromatographic apparatusused in that separation step.

Typically, in this particularly preferred embodiment, the rate at whichliquid collected via the extract stream in the first separation step isrecycled back into the chromatographic apparatus used in the firstseparation step is faster than the rate at which liquid collected viathe extract stream in the second separation step is recycled back intothe chromatographic apparatus used in the second separation step.

In this particularly preferred embodiment the first raffinate stream inthe first separation step is typically removed downstream of the pointof introduction of the feed mixture into the chromatographic apparatusused in the first separation step, with respect to the flow of eluent.

In this particularly preferred embodiment, the first extract stream inthe first separation step is typically removed upstream of the point ofintroduction of the feed mixture into the chromatographic apparatus usedin the first separation step, with respect to the flow of eluent.

In this particularly preferred embodiment, the second raffinate streamin the second separation step is typically removed downstream of thepoint of introduction of the intermediate product into thechromatographic apparatus used in the second separation step, withrespect to the flow of eluent.

In this particularly preferred embodiment, the second extract stream inthe second separation step is typically collected upstream of the pointof introduction of the intermediate product into the chromatographicapparatus used in the second separation step, with respect to the flowof eluent.

Typically in this particularly preferred embodiment, the organic solventor aqueous organic solvent is introduced into the chromatographicapparatus used in the first separation step upstream of the point ofremoval of the first extract stream, with respect to the flow of eluent.

Typically in this particularly preferred embodiment, when water isintroduced into the chromatographic apparatus used in the firstseparation step, the water is introduced into the chromatographicapparatus used in the first separation step upstream of the point ofintroduction of the feed mixture but downstream of the point of removalof the first extract stream, with respect to the flow of eluent.

Typically in this particularly preferred embodiment, the organic solventor aqueous organic solvent is introduced into the chromatographicapparatus used in the second separation step upstream of the point ofremoval of the second extract stream, with respect to the flow ofeluent.

Typically in this particularly preferred embodiment, when water isintroduced into the chromatographic apparatus used in the secondseparation step, the water is introduced into the chromatographicapparatus used in the second separation step upstream of the point ofintroduction of the intermediate product but downstream of the point ofremoval of the second extract stream, with respect to the flow ofeluent.

Particularly preferred embodiment (2) is suitable for purifying DHA froma feed mixture.

Particularly preferred embodiment (2) is illustrated in FIG. 3. A feedmixture F comprising the PUFA product (B) and more polar (C) and lesspolar (A) components is purified in the first separation step. In thefirst separation step, the more polar components (C) are removed asraffinate stream R1. The PUFA product (B) and less polar components (A)are collected as extract stream E1. Extract stream E1 is theintermediate product which is then purified in the second separationstep. In the second separation step, the less polar components (A) areremoved as extract stream E2. The PUFA product (B) is collected asraffinate stream R2.

This embodiment is illustrated in more detail in FIG. 5. FIG. 5 isidentical to FIG. 3, except that the points of introduction of theorganic solvent desorbent (D) and water (W) into each chromatographicapparatus are shown. As above, the (D) phase is typically essentiallypure organic solvent, but may, in certain embodiments be an organicsolvent/water mixture comprising mainly organic solvent. The (W) phaseis typically essentially pure water, but may, in certain embodiments bean organic solvent/water mixture comprising mainly water, for example a98% water/2% methanol mixture.

A further illustration of this particularly preferred embodiment isshown in FIG. 7. Here there is no separate water injection point, andinstead an aqueous organic solvent desorbent is injected at (D).

Typical solvents for use in this most preferred embodiment are aqueousalcohols or aqueous acetonitrile, preferably aqueous methanol.

Typically in this embodiment, the rate at which liquid collected via theraffinate stream in the first separation step is reintroduced into thechromatographic apparatus used in the first separation step is fasterthan the rate at which liquid collected via the raffinate stream in thesecond separation step is reintroduced into the chromatographicapparatus used in the second separation step.

In this embodiment the first raffinate stream in the first separationstep is typically removed downstream of the point of introduction of thefeed mixture into the chromatographic apparatus used in the firstseparation step, with respect to the flow of eluent.

In this embodiment, the first extract stream in the first separationstep is typically removed upstream of the point of introduction of thefeed mixture into the chromatographic apparatus used in the firstseparation step, with respect to the flow of eluent.

In this embodiment, the second raffinate stream in the second separationstep is typically removed downstream of the point of introduction of theintermediate product into the chromatographic apparatus used in thesecond separation step, with respect to the flow of eluent.

In this embodiment, the second extract stream in the second separationstep is typically collected upstream of the point of introduction of theintermediate product into the chromatographic apparatus used in thesecond separation step, with respect to the flow of eluent.

Typically in this embodiment, the organic solvent or aqueous organicsolvent is introduced into the chromatographic apparatus used in thefirst separation step upstream of the point of removal of the firstextract stream, with respect to the flow of eluent.

Typically in this embodiment, when water is introduced into thechromatographic apparatus used in the first separation step, the wateris introduced into the chromatographic apparatus used in the firstseparation step upstream of the point of introduction of the feedmixture but downstream of the point of removal of the first extractstream, with respect to the flow of eluent.

Typically in this embodiment, the organic solvent or aqueous organicsolvent is introduced into the chromatographic apparatus used in thesecond separation step upstream of the point of removal of the secondextract stream, with respect to the flow of eluent.

Typically in this embodiment, when water is introduced into thechromatographic apparatus used in the second separation step, the wateris introduced into the chromatographic apparatus used in the secondseparation step upstream of the point of introduction of theintermediate product but downstream of the point of removal of thesecond extract stream, with respect to the flow of eluent.

In a preferred embodiment of the invention, each of the simulated oractual moving bed chromatography apparatus used in the first and secondseparation steps consist of eight chromatographic columns. These arereferred to as columns 1 to 8. In each apparatus the eight columns arearranged in series so that the bottom of column 1 is linked to the topof column 2, the bottom of column 2 is linked to the top of column 3 . .. etc. . . . and the bottom of column 8 is linked to the top ofcolumn 1. These linkages may optionally be via a holding container, witha recycle stream into the next column. The flow of eluent through thesystem is from column 1 to column 2 to column 3 etc. The effective flowof adsorbent through the system is from column 8 to column 7 to column 6etc.

A most preferred embodiment is illustrated in FIG. 8. A feed mixture Fcomprising the PUPA product (B) and more polar (C) and less polar (A)components is introduced into the top of column 5 in the chromatographicapparatus used in the first separation step. Organic solvent desorbentis introduced into the top of column 1 of the chromatographic apparatusused in the first separation step. Water is introduced into the top ofcolumn 4 of the chromatographic apparatus used in the first separationstep. In the first separation step, the less polar components (A) areremoved as extract stream E1 from the bottom of column 2. The PUFAproduct (B) and more polar components (C) are removed as raffinatestream R1 from the bottom of column 7. Raffinate stream R1 is theintermediate product which is then purified in the second separationstep, by being introduced into the chromatographic apparatus used in thesecond separation step at the top of column 5. Organic solvent desorbentis introduced into the top of column 1 in the chromatographic apparatusused in the second separation step. Water is introduced into the top ofcolumn 4 in the chromatographic apparatus used in the second separationstep. In the second separation step, the more polar components (C) areremoved as raffinate stream R2 at the bottom of column 7. The PUFAproduct (B) is collected as extract stream E2 at the bottom of column 2.

In this most preferred embodiment, organic solvent is typicallyintroduced into the top of column 1 of the chromatographic apparatusused in the first separation step.

In this most preferred embodiment, water is typically introduced intothe top of column 4 of the chromatographic apparatus used in the firstseparation step.

In this most preferred embodiment, organic solvent is typicallyintroduced into the top of column 1 of the chromatographic apparatusused in the second separation step.

In this most preferred embodiment, organic solvent is typicallyintroduced into the top of column 4 of the chromatographic apparatusused in the second separation step.

In this most preferred embodiment, the feed stream is typicallyintroduced into the top of column 5 of the chromatographic apparatusused in the first separation step.

In this most preferred embodiment, a first raffinate stream is typicallycollected as the intermediate product from the bottom of column 7 of thechromatographic apparatus used in the first separation step. Thisintermediate product is then purified in the second separation step andis typically introduced into the top of column 5 of the chromatographicapparatus used in the second separation step. The first raffinate streammay optionally be collected in a container before being purified in thesecond separation step.

In this most preferred embodiment, a first extract stream is typicallyremoved from the bottom of column 2 of the chromatographic apparatusused in the first separation step. The first extract stream mayoptionally be collected in a container and reintroduced into the top ofcolumn 3 of the chromatographic apparatus used in the first separationstep.

In this most preferred embodiment, a second raffinate stream istypically removed from the bottom of column 7 of the chromatographicapparatus used in the second separation step.

In this most preferred embodiment, a second extract stream is typicallycollected from the bottom of column 2 of the chromatographic apparatusused in the second separation step. This second extract stream typicallycontains the purified PUFA product. The second extract stream mayoptionally be collected in a container and reintroduced into the top ofcolumn 3 of the chromatographic apparatus used in the second separationstep.

In this most preferred embodiment, the eluent used is typically aqueousalcohol, preferably aqueous methanol. The water:alcohol ratio istypically from 0.5:99.5 to 6:94 parts by volume.

In this most preferred embodiment, the rate at which liquid collectedvia the extract stream from the first separation step is recycled backinto the chromatographic apparatus used in the first separation step istypically faster than the rate at which liquid collected via the extractstream from the second separation step is recycled back into thechromatographic apparatus used in the second separation step.

In this most preferred embodiment, the aqueous organic solvent eluent issubstantially the same in each separation step.

Although the embodiment of FIG. 8 is configured as shown in FIG. 10 a,the configurations shown in FIGS. 10 b and 10 c could also be used inthis embodiment.

A further most preferred embodiment is illustrated in FIG. 9. A feedmixture F comprising the PUFA product (B) and more polar (C) and lesspolar (A) components is introduced into the top of column 5 in thechromatographic apparatus used in the first separation step. Aqueousorganic solvent desorbent is introduced into the top of column 1 in thechromatographic apparatus used in the first separation step. In thefirst separation step, the less polar components (A) are removed asextract stream E1 from the bottom of column 2. The PUFA product (B) andmore polar components (C) are removed as raffinate stream R1 from thebottom of column 7. Raffinate stream R1 is the intermediate productwhich is purified in the second separation step by being introduced intothe top of column 4 of the chromatographic apparatus used in the secondseparation step. Aqueous organic solvent desorbent is introduced intothe top of column 1 in the chromatographic apparatus used in the secondseparation step. In the second separation step, the more polarcomponents (C) are removed as raffinate stream R2 at the bottom ofcolumn 7. The PUFA product (B) is collected as extract stream E2 at thebottom of column 2.

In this most preferred embodiment, aqueous organic solvent is typicallyintroduced into the top of column 1 in the chromatographic apparatusused in the first separation step.

In this most preferred embodiment, aqueous organic solvent is typicallyintroduced into the top of column 9 in the chromatographic apparatusused in the second separation step.

In this most preferred embodiment, the feed stream is typicallyintroduced into the top of column 5 in the chromatographic apparatusused in the first separation step.

In this most preferred embodiment, a first raffinate stream is typicallycollected as the intermediate product from the bottom of column 7 of thechromatographic apparatus used in the first separation step. Thisintermediate product is then purified in the second separation step andis typically introduced into the top of column 5 of the chromatographicapparatus used in the second separation step. The first raffinate streammay optionally be collected in a container before being purified in thesecond separation step.

In this most preferred embodiment, a first extract stream is typicallyremoved from the bottom of column 2 of the chromatographic apparatusused in the first separation step. The first extract stream mayoptionally be collected in a container and a portion reintroduced intothe top of column 3 of the chromatographic apparatus used in the firstseparation step. The rate of recycle of liquid collected via the extractstream in the first separation step back into the chromatographicapparatus used in the first separation step is the rate at which liquidis pumped from this container into the top of column 3.

In this most preferred embodiment, a second raffinate stream istypically removed from the bottom of column 7 of the chromatographicapparatus used in the first separation step.

In this most preferred embodiment, a second extract stream is typicallycollected from the bottom of column 2 of the chromatographic apparatusused in the first separation step. This second extract stream typicallycontains the purified PUFA product. The second extract stream mayoptionally be collected in a container and a portion reintroduced intothe top of column 3 of the chromatographic apparatus used in the firstseparation step. The rate of recycle of liquid collected via the extractstream from the second separation step back into the chromatographicapparatus used in the second separation step is the rate at which liquidis pumped from this container into the top of column 3.

In this most preferred embodiment, the eluent used is typically aqueousalcohol, preferably aqueous methanol. The water:alcohol ratio istypically from 0.5:99.5 to 6:94 parts by volume.

In this most preferred embodiment, the rate at which liquid collectedvia the extract stream from the first separation step is recycled backinto the chromatographic apparatus used in the first separation step istypically faster than the rate at which liquid collected via the extractstream from the second separation step is recycled back into thechromatographic apparatus used in the second separation step.

In this most preferred embodiment, the aqueous organic solvent eluent issubstantially the same in each separation step.

Although the embodiment of FIG. 9 is configured as shown in FIG. 10 a,the configurations shown in FIGS. 10 b and 10 c could also be used inthis embodiment.

The process of the invention allows much higher purities of PUFA productto be achieved than have been possible with conventional chromatographictechniques. PUFA products produced by the process of the invention alsohave particularly advantageous impurity profiles, which are quitedifferent from those observed in oils prepared by known techniques. Thepresent invention therefore also relates to compositions comprising aPUFA product, for example one obtainable by the process of the presentinvention.

In practice, the process of the present invention will generally becontrolled by a computer. The present invention therefore also providesa computer program for controlling a chromatographic apparatus asdefined herein, the computer program containing code means that whenexecuted instruct the apparatus to carry out the process of theinvention.

The following Examples illustrate the invention.

EXAMPLES Example 1

A fish oil derived feedstock (55 weight % EPA EE, 5 weight % DHA EE) isfractionated using an actual moving bed chromatography system usingbonded C18 silica gel (particle size 300 microns, particle porosity 150angstroms) as stationary phase and aqueous methanol (containing 7.5%water) as eluent according to the system schematically illustrated inFIG. 9.

The first separation step was carried out on an SMB apparatus having 8columns (diameter: 76.29 mm, length: 914.40 mm) which are connected inseries as shown in FIG. 9. The intermediate product raffinate from thefirst separation step was isolated and purified in a second separationstep using the same sequence of columns as above.

EPA was produced with purity 97%

The operating parameters and flow rates are as follows.

Step time: 500 secs

Cycle time: 133.33 mins

First Separation Step

Feedstock (F) feed rate: 25 ml/min

Desorbent feed rate (D1): 2050 ml/min

Extract container accumulation rate (E1): 1125 ml/min

Extract recycle rate (D1-E1): 925 ml/min

Raffinate rate (R1): 950 ml/min

Second Separation Step

Desorbent feed rate (D2): 1700 ml/min

Extract container accumulation rate (E2): 900 ml/min

Extract recycle rate (D2-E2): 800 ml/min

Raffinate rate (R2): 800 ml/min

A GC trace of the EPA feedstock is shown as FIG. 11.

A GC trace of the raffinate intermediate product obtained in the firstseparation step is shown as FIG. 12.

A GC trace of the final EPA product is shown as FIG. 13.

Example 2

A fish oil derived feedstock (55 weight % EPA EE, 5 weight % DHA EE) isfractionated using an actual moving bed chromatography system usingbonded C18 silica gel (particle size 300 microns, particle porosity 150angstroms) as stationary phase and aqueous methanol (containing 8 wt %water) as eluent according to the system schematically illustrated inFIG. 9, except that a fifteen column array was used instead of an eightcolumn array.

The first separation step was carried out on an SMB apparatus having 15columns (diameter: 150 mm, length: 813 mm) which are connected in seriesas shown in FIG. 9. The intermediate product from the first separationstep was isolated and purified in a second separation step using thesame sequence of columns as above.

EPA was produced with purity 98%.

Step time: 1200 secs

First Separation Step

Feed (F): 35 ml/min

Desorb (D1): 2270 ml/min

Extract separation E1: 1320 ml/min

Extract recycle rate (D1-E1): 950 ml/min

Raffinate separation R1: 950 ml/min

Second Separation Step

Desorb (D2): 1510 ml/min

Extract separation E2: 850 ml/min

Extract recycle rate (D2-E2): 660 ml/min

Raffinate separation R2: 670 ml/min

A GC trace of the EPA product produced is shown as FIG. 14.

Reference Example 1

An experiment was carried out to compare the amount of environmentalpollutants present in two PUFA products produced by SMB with similaroils prepared by distillation. The pollutant profiles of the oils areshown in Table 1 below.

TABLE 1 PUFA product PUFA product Release Distilled Distilled producedby produced by Parameter Specification oil [1] oil [2] SMB [1] SMB [2]Polyaromatic Hydrocarbons (PAH) (μg/kg) Benzo(a)pyrene NMT 2.0 0.90 0.90<0.05 <0.05 Impurities Dioxins and Furans PCDDs and NMT 2.0 0.46 0.370.2 0.184 PCDFs¹⁾ (pg WHO-PCDD/F-TEQ/g) PCBs (mg/kg) NMT 0.09 0.00370.0103 0.0007 0.0012 Sum of Dioxins, Furans and Dioxin- NMT 10.0 1.030.466 0.30 0.298 like PCBs²⁾ (pg WHO-PCDD/F-PCB-TEQ/g) ¹⁾Dioxin limitsinclude the sum of polychlorinated dibenzeno-para-dioxins (PCDDs) andpolychlorinated dibenzofurans (PCDFs) and expressed in World HealthOrganisation (WHO) toxic equivalents using WHO-toxic equivalent factors(TEFs). This means that analytical results relating to 17 individualdioxin congeners of toxicological concern are expressed in a singlequantifiable unit: TCDD toxic equivalent concentration or TEQ ²⁾Maximumfor dioxin and Furans remains at 2 pg/g

Reference Example 2

An experiment was carried out to determine the amount of isomericimpurities present in an oil prepared by SMB compared with an equivalentoil prepared by distillation.

A GC trace of the DHA-rich oil prepared by SMB is shown as FIG. 15.There is no evidence of isomeric impurities in the GC trace.

A GC trace of the oil prepared by distillation is shown as FIG. 16. Thefour peaks with longer elution times than the DHA peak correspond to DHAisomers. From the

GC trace it can be seen that the oil prepared by distillation containsabout 1.5 wt % of isomeric impurities.

Reference Example 3

Two EPA-rich products produced by SMB were compared with EPA-rich oilsproduced by distillation. The wt % analysis of their component PUFAs isshown below.

PUFA product PUFA product produced by produced by Distilled DistilledFatty Acid SMB [1] SMB [2] oil [1] oil [2] EPA (C20:5n-3) 98.33  97.04 98.09  98.14  DHA (C22:6n-3) 0.15 <LOD 0.34 <LOD C18:3 n-3 <LOD 0.280.24 <LOD C18:4 n-3 0.33 0.20 0.14 0.26 C20:4 n-3 0.14 0.45 0.18 0.46C21:5 n-3 <LOD <LOD <LOD <LOD C22:5 n-3 0.32 <LOD <LOD <LOD TotalOmega-3 99.27  97.97  98.94  98.86  C18:3n-6 <LOD <LOD 0.05 <LOD C20:3n-6 <LOD <LOD 0.13 0.11 C20:4 n-6 <LOD 0.21 0.26 0.37 Total Omega-6 <LOD0.21 0.44 0.48

Reference Example 4

An EPA/DHA-rich product produced by SMB was compared with anEPA/DHA-rich oil produced by distillation. The wt % analysis of theircomponent PUFAs is shown below.

Maxomega Ethyl Ester Distilled Ethyl Ester (Omega-3 90 ethyl (Omega-3 90ethyl esters) esters¹) Fatty Acid Area % Area % EPA (C20:5n-3) 53.3 46.6DHA (C22:6n-3) 32.9 38.2 TOTAL EPA + 86.2 84.8 DHA C18:3 n-3 0.3 0.1C18:4 n-3 1.2 2.0 C20:4 n-3 1.8 0.6 C21:5 n-3 2.7 1.8 C22:5 n-3 5.0 3.8Total Omega-3 97.2 93.1 C18:2 n-6 0.2 0.1 C18:3n-6 <0.1 0.2 C20:3 n-6<0.1 0.1 C20:4 n-6 2.0 2.6 C22:4 n-6 <0.1 0.1 C22:5 n-6 0.6 1.0 TotalOmega-6 2.8 4.1

1. A chromatographic separation process for recovering a polyunsaturatedfatty acid (PUFA) product from a feed mixture, which process comprisesthe steps of: (i) purifying the feed mixture in a first separation stepin a simulated or actual moving bed chromatography apparatus having aplurality of linked chromatography columns containing, as eluent, anaqueous organic solvent, to obtain an intermediate product; and (ii)purifying the intermediate product obtained in (i) in a secondseparation step using a simulated or actual moving bed chromatographyapparatus having a plurality of linked chromatography columnscontaining, as eluent, an aqueous organic solvent, to obtain the PUFAproduct; wherein (a) the first and second separation steps are carriedout sequentially on the same chromatography apparatus, the intermediateproduct being recovered between the first and second separation stepsand the process conditions in the chromatography apparatus beingadjusted between the first and second separation steps such that thePUFA product is separated from different components of the feed mixturein each separation step; or (b) the first and second separation stepsare carried out on separate first and second chromatography apparatusesrespectively, the intermediate product obtained from the firstseparation step being introduced into the second chromatographyapparatus, and the PUFA product being separated from differentcomponents of the feed mixture in each separation step; and wherein (1)part of an extract stream from the apparatus used in the firstseparation step is recycled back into the apparatus used in the firstseparation step; and/or (2) part of a raffinate stream from theapparatus used in the first separation step is recycled back into theapparatus used in the first separation step; and/or (3) part of anextract stream from the apparatus used in the second separation step isrecycled back into the apparatus used in the second separation step;and/or (4) part of a raffinate stream from the apparatus used in thesecond separation step is recycled back into the apparatus used in thesecond separation step, and wherein (I) a rate at which liquid collectedvia one or both of the extract and raffinate streams in the firstseparation step is recycled back into the apparatus used in thatseparation step is adjusted such that the PUFA product can be separatedfrom different components of the feed mixture in each separation step;and/or (II) a rate at which liquid collected via one or both of theextract and raffinate streams in the second separation step is recycledback into the apparatus used in that separation step is adjusted suchthat the PUFA product can be separated from different components of thefeed mixture in each separation step.
 2. The process according to claim1, wherein each apparatus has an extract stream and a raffinate streamfrom which liquid can be collected from said plurality of linkedchromatography columns.
 3. The A process according to claim 1, whereinthe intermediate product obtained in the first separation step isenriched in the PUFA product compared to the feed mixture.
 4. The Aprocess according to claim 1, wherein (a) the intermediate product iscollected as the raffinate stream in the first separation step, and thePUFA product is collected as the extract stream in the second separationstep; or (b) the intermediate product is collected as the extract streamin the first separation step, and the PUFA product is collected as theraffinate stream in the second separation step.
 5. The A processaccording to claim 1, wherein the PUFA product is separated from lesspolar components of the feed mixture in the first separation step, andthe PUFA product is separated from more polar components of the feedmixture in the second separation step.
 6. The A process according toclaim 1, wherein the PUFA product comprises at least one ω-3 PUFA. 7.The A process according to claim 6, wherein the PUFA product comprisesEPA and/or DHA.
 8. The A process according to claim 1, wherein theeluent is a mixture of water and an alcohol, an ether, an ester, aketone or a nitrile.
 9. The A process according to claim 8, wherein theeluent is a mixture of water and methanol.
 10. The A process accordingto claim 1, wherein the feed mixture is a fish oil or fish-oil derivedfeedstock, the PUFA product is EPA or EPA ethyl ester, and the PUFAproduct is produced in a purity greater than 90% purity, preferablygreater than 95% purity, and more preferably greater than 97% purity.11.-13. (canceled)
 14. The A process according to claim 1, wherein therate at which liquid collected via the extract stream in the firstseparation step is recycled back into the chromatography apparatus usedin the first separation step differs from the rate at which liquidcollected via the extract stream in the second separation step isrecycled back into the chromatography apparatus used in the secondseparation step.
 15. The A process according to claim 1, wherein therate at which liquid collected via the raffinate stream in the firstseparation step is recycled back into the chromatography apparatus usedin the first separation step differs from the rate at which liquidcollected via the raffinate stream in the second separation step isrecycled back into the chromatography apparatus used in the secondseparation step.
 16. The A process according to claim 1, wherein therate at which liquid collected via the extract stream in the firstseparation step is recycled back into the chromatographic apparatus usedin the first separation step is faster than the rate at which liquidcollected via the extract stream in the second separation step isrecycled back into the chromatographic apparatus used in the secondseparation step.
 17. A computer program for controlling a chromatographyapparatus according to claim 1, which computer program contains codemeans that, when executed, instructs the apparatus to carry out aprocess according to claim
 1. 18. A PUFA product produced by the processof claim 1.